EP1474364A1 - Method and device for desalination of water and removal of carbon dioxide from exhaust gases - Google Patents

Method and device for desalination of water and removal of carbon dioxide from exhaust gases

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Publication number
EP1474364A1
EP1474364A1 EP03703551A EP03703551A EP1474364A1 EP 1474364 A1 EP1474364 A1 EP 1474364A1 EP 03703551 A EP03703551 A EP 03703551A EP 03703551 A EP03703551 A EP 03703551A EP 1474364 A1 EP1474364 A1 EP 1474364A1
Authority
EP
European Patent Office
Prior art keywords
exhaust
process unit
gas turbine
feed pipe
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP03703551A
Other languages
German (de)
French (fr)
Other versions
EP1474364B1 (en
Inventor
Knut Erik B Rseth
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sargas AS
Original Assignee
Fleischer & Co As
Kebmar AS
Sargas AS
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Application filed by Fleischer & Co As, Kebmar AS, Sargas AS filed Critical Fleischer & Co As
Publication of EP1474364A1 publication Critical patent/EP1474364A1/en
Application granted granted Critical
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/102—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B01D2252/1035—Sea water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/45—Gas separation or purification devices adapted for specific applications
    • B01D2259/4566—Gas separation or purification devices adapted for specific applications for use in transportation means
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the invention relates to an improved process for removal of C0 2 from exhaust gases, in which huge amounts of seawater are transformed to fresh water by addition of ammonia NH 3 with subsequent precipitation of sodium hydrogen carbonate NaHC0 3 and ammonium chloride NH 4 CI.
  • the process is made more efficient by using air, seawater and steam as heat sources during 0 evaporation of liquefied natural gas (LNG). Cooled air is provided for the air inlet of a gas turbine, a feature that considerably improves the efficiency. Cooled seawater is used for removal of C0 2 from the exhaust gas from the gas turbine. This process is made more efficient by having a low seawater temperature; about 10 °C. Steam is generated in the exhaust boiler of the gas turbine. The 5 gas turbine generates electrical power for running the process that is necessary for evaporation of LNG. The excess electrical power is exported.
  • LNG liquefied natural gas
  • a typical gas turbine of 25 Megawatt (MW) generates an exhaust flow of about 3,3 kg/s of C0 2 . That represents a large and undesirable production of C0 2 considering the probable contributions to greenhouse effects on the global atmosphere. Further, we expect that the unified process according to the invention also will prove commercially healthy because several countries may incur official C0 2 -fees and / or trade C0 2 emission permissions, so-called "green certificates".
  • the process according to a preferred embodiment of the invention has its greatest potential in those parts of the world in which there is a lack of fresh water, e.g. in the Middle East, Western Africa, The Read Sea, etc.
  • One of the main purposes of the invention is to contribute to the use of liquefied natural gas (LNG), seawater and ammonia for an electricity production of significantly reduced CCVemission, and evaporation of LNG simultaneously with soda production and fresh water production, in which all the products have a sales value.
  • LNG liquefied natural gas
  • the invention also improves the efficiency of the electricity production from the gas turbine, by cooling the air to the gas turbine by means of LNG, the invention represents an essential improvement for efficient use of the Solvay process. Further, the process is dependent of low sea water temperature in order to achieve efficient removal of C0 2 , about 10 °C.
  • the invention is a method for desalination of salt water, preferably seawater, and separation of C0 2 from a C0 2 -rich exhaust gas from a fuel combustion engine or gas turbine, comprising the following steps:
  • LNG is fed into a heat exchanger in which heat is taken from seawater and heat from steam from a steam turbine, and heat from combustion air via a line to the air inlet to a gas turbine, for evaporating LNG to gas being fed to a gas export module and to a fuel gas skid for providing the gas turbine with fuel;
  • the combustion air which at the air supply to the gas turbine thus has a lowered temperature, and thus increases the efficiency of the gas turbine;
  • C0 2 -rich exhaust gas from the gas turbine is led into a chamber or process unit having an inlet with a fan and an outlet for C0 2 -removed exhaust;
  • the cooled salt water from the heat exchanger is fed into the process unit via an upper swivel having vanes that rotates a coaxial feed pipe for seawater and NH 4 OH, said coaxial pipe being arranged preferably in a centre line in said process unit;
  • the invention is also a process unit for removing CO2 from an exhaust from a combustion engine or gas turbine, comprising the following features: an inlet with a fan and an outlet for exhaust of reduced C0 2 content; in which cooled salt water can be piped into said process unit via an upper swivel having vanes for rotating a coaxial pipe, said coaxial pipe for seawater and NH4OH feed, said coaxial feed pipe being arranged preferably in a centre line of said process unit; in which NH4OH can be guided in via a lower swivel on said coaxial pipe and mixed with said cooled salt water and released via a series of nozzles from said feed pipe, said nozzles arranged in several vertical levels, to upwardly flowing and rotating exhaust of said process unit; thus for achieving a mixture of NH 4 OH -containing salt water and C0 2 -rich exhaust for formation of NaHC0 3 , NH CI and desalinated water.
  • Fig. 1 illustrates a plan section of the terminal limits or process area 26, and illustrates in-flowing fluids and dry matter to the process from the left side in the drawing, with products from the products at the right side in the drawing.
  • Chalk Ca(OH) 2 (1) is sent to the process unit for regenerating of ammonia NH 3 (19), which will be explained below.
  • Ammonia (2) is sent to a mixing unit for seawater and ammonia, for formation of NH OH for injection via an insert feed pipe (67) to a process unit (17) for removal of C0 2 from exhaust gas (77) from a gas turbine (7), resulting in release of cleaned exhaust gas (13) to the atmosphere.
  • Central for the preparation to the process is one or more heat exchangers (6). Combustion air of ambient temperature, e.g. 20-35 °C, is led into the heat exchanger.
  • LNG (4) receives heat from the combustion air (3), and from seawater (5) and from steam from the exhaust gas steam boiler (18), steam of which is also piped through the heat exchanger.
  • Boil-off gas (73) from the storage tank (80) may also be guided in through the heat exchanger if heating is needed before it is fed into the gas skid module (8) to constitute fuel for the gas turbine (7).
  • Possible excess boil-off gas (73) may be fed into a line (29) to a gas export module (10).
  • the heat exchanger (6) is arranged before the gas turbine (7) and the process unit (17) constituting an exhaust process tower (17) for adsorbing C0 2 from the exhaust, leading further to a precipitation process unit for fresh water at the right side of the drawing.
  • the process is, according to a preferred embodiment, a method for desalination of salt water (5), which may be seawater or brackish water, with separation of C0 2 from a C0 2 -rich exhaust (77) from a combustion engine, boiler or gas turbine (7).
  • the process comprises the following steps:
  • LNG (4) is fed into the heat exchanger (6) in which it receives heat from the seawater (5) and heat from steam (27) from a steam turbine (31), and also heat from combustion air (3) sent via a line (28) to the air inlet (33) to the gas turbine (7).
  • LNG (4) will then receive heat and evaporate to gas (29) that is led to a gas export module (10) and to a fuel gas skid (8) for providing the gas turbine (7) with fuel.
  • the combustion air (28) at the air inlet (33) to the gas turbine (7) thereby is lowered in temperature out of the heat exchanger due to being cooled down by LNG (4), and thus increases the efficiency of the gas turbine (7).
  • C0 2 -rich exhaust gas (77) from the gas turbine (7) is led into a chamber rather called a process unit (17) having an inlet (35a) provided with a fan (35b) in the lower portion of the process unit (17), and an outlet (74) for C0 2 -removed exhaust (13) at the upper end of the process unit (17).
  • the cooled salt water (30) from the heat exchanger (6) is fed into the process unit (17) via an upper swivel (40) having vanes that rotate an insert coaxial pipe (67) for seawater and NH 4 OH in a desired direction (71) being opposite of the desired rotation direction (72) for the exhaust gas, and preferably being arranged along the centre line inside the process unit (17).
  • This increases the degree of mixing between the seawater mixture and the exhaust gas considerably compared to the US Patent 6 180 012.
  • NH OH is led in through a lower swivel (46) on the coaxial pipe (67).
  • NH4OH is mixed with the cooled salt water (30) and flushed out into the process unit (17) via a series of radially directed nozzles (42) at several vertical levels from the coaxial pipe (67) to the upwardly flowing, rotating exhaust (77) through the process unit (17).
  • C0 2 -lean exhaust 13
  • the process unit (17) has a diameter increasing with increased elevation from the lower inlet (35a) to the upper outlet (74). Drain gutters (38) to drains (43) are arranged, leading to outlets (45) to a collecting tank (48) for NaHCC»3, NH4CI, and fresh water.
  • an exhaust fan (35B) forcing forward the exhaust (77) and thus reduces the counter pressure for the gas turbine (7) so as to compensate the pressure drop through the process unit (17) in order to maintain the efficiency of the gas turbine.
  • the exhaust fan (35B) initiates at the same time a rotation of the exhaust gas (77), further reinforced by means of fixed guide vanes (36) arranged downstream at the inlet (35a) of the process unit (17).
  • NH 4 OH enters through the lower swivel (46) to a central, coaxial inner pipe (47) in the coaxial feed pipe (67) in the process unit (17).
  • the inner pipe (47) is surrounded by a mantle of salt water (30) through which NH 4 OH is led out through pipes to sea water ring nozzles (42) in the feed pipe (67).
  • NH 4 OH and seawater are mixed through flushing from the nozzles to the C ⁇ 2 -rich exhaust (77) gradually being changed to C0 2 -lean exhaust (13) on its way upward through the process unit (17).
  • the nozzles are preferably provided with NH 4 OH- radial distributors (70) arranged just outside the nozzles (42) in order for NH OH to be forced out through an enveloping flow of the mixed cooled seawater (30).
  • NH 4 OH- radial distributors 70
  • Precipitated material of NaHC0 3 , NH 4 CI intermediately dissolved in H 2 0 are conducted to a precipitator (22) for separation of NaHC0 3 and NH CI from the water H 2 0 which is generally pure fresh water if the process is thoroughly controlled and low temperature of the seawater is maintained.
  • a precipitator for separation of NaHC0 3 and NH CI from the water H 2 0 which is generally pure fresh water if the process is thoroughly controlled and low temperature of the seawater is maintained.
  • the precipitator is generally pure fresh water if the process is thoroughly controlled and low temperature of the seawater is maintained.
  • (22) is vertically standing and cylindrical, and has a rotation-inducing tangential inlet (25B) for NaHC0 2 / NH4CI dissolved in water.
  • the driving pressure is generated from the pressure head from the collector tank (48) to the inlet (25B).
  • NaHC0 2 / NH4CI is precipitated by the rotation and the gravitation towards the bottom of the precipitator (22).
  • fresh water (74) is taken out through a fresh water overflow pipe (75) to a fresh water filter tank (62).
  • the fresh water (74) from the filter tank (62) is sent through a filter (61) to a distribution- and settling tank (60).
  • Salt water may be present at the bottom of the settling tank (60), of which salt water may be lifted back to the seawater pipe (30) by means of the pump (53).
  • Fresh water (74) is pumped by means of the pump (54) to storage tank (59), and further from storage tank (59) via discharge pump (58) and booster pump / export pump (56) to an export pipeline (14).
  • the precipitated NH CI and NaHC0 3 is lifted by means of a screw pump or "archimedes screw” (51) that is driven by a motor (50), to an outlet (76) from the precipitator (22) to a refining process compartment (64).
  • Chalk Ca(OH) 2 (1) is led into the process unit (20) for regeneration of ammonia NH 3 that is fed via a pipe (19) to be mixed with additional NH 3 (2) from the ammonia tank (65).
  • the ammonia (2, 19) is led further to the mixing unit (32) mixing salt water and ammonia (2, 19) and pumps the mixture NH OH into the feed pipe (67) in the process unit (17).
  • the gas turbine (7) drives a generator (9) for generating electrical energy that partially may be exported as energy (15), and partially to be used for pumping work, gas and /or C0 2 export work, and heating a process unit (24) that precipitates soda / Na 2 C0 3 (12) for export, and C0 2 and fresh water, which are exported or returned to the process.
  • a generator 9 for generating electrical energy that partially may be exported as energy (15), and partially to be used for pumping work, gas and /or C0 2 export work, and heating a process unit (24) that precipitates soda / Na 2 C0 3 (12) for export, and C0 2 and fresh water, which are exported or returned to the process.
  • LNG liquefied natural gas
  • -163 °C (1 ,2 mill, tons/year.

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  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
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  • Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
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  • Organic Chemistry (AREA)
  • Treating Waste Gases (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Physical Water Treatments (AREA)

Abstract

This invention relates to a method for desalination of seawater (5, 30) and separation of C02 from exhaust (77) from a gas turbine (7). LNG (4) is fed into a heat exchanger (6) in which it receives heat from seawater (5) and heat from steam (27) from an exhaust boiler, and heat from combustion air (3) via a line to an air inlet (33) of said gas turbine (7), for evaporating LNG (4) to gas which is fed to a gas export module (10) and to a fuel gas skid (8) for supplying said gas turbine (7) with fuel. Thus said combustion air (3, 28) at the air inlet to said gas turbine (7) obtains a lowered temperature and increases an efficiency of said gas turbine (7). Said C02-rich exhaust gas (77) from said gas turbine (7) is fed into a process unit (17) having an inlet (35a) with a fan (35b) and an outlet for C02-reduced exhaust (13). Said cooled seawater from said heat exchanger (6) is fed into said process unit (17) via a coaxial feed pipe (67) for seawater and NH40H arranged in said process unit (17). NH40H is fed into said coaxial feed pipe (67) and is then mixed with said cooled seawater (30) and released via a series of nozzles in several vertical levels from said feed pipe (67) to said process unit's (17) upwards flowing, rotating exhaust (77). By this device a good mixture of NH40H - containing salt water and C02-rich exhaust is achieved, for formation of NaHC03, NH4CI, and fresh water.

Description

Method and device for desalination of water and removal of carbon dioxide from exhaust gases .
Introduction. 5 The invention relates to an improved process for removal of C02 from exhaust gases, in which huge amounts of seawater are transformed to fresh water by addition of ammonia NH3 with subsequent precipitation of sodium hydrogen carbonate NaHC03 and ammonium chloride NH4CI. The process is made more efficient by using air, seawater and steam as heat sources during 0 evaporation of liquefied natural gas (LNG). Cooled air is provided for the air inlet of a gas turbine, a feature that considerably improves the efficiency. Cooled seawater is used for removal of C02 from the exhaust gas from the gas turbine. This process is made more efficient by having a low seawater temperature; about 10 °C. Steam is generated in the exhaust boiler of the gas turbine. The 5 gas turbine generates electrical power for running the process that is necessary for evaporation of LNG. The excess electrical power is exported.
Known art in the field.
Precipitation of NaHC03 and NH4CI as described above is, in its basic 0 principle, known as the Solvay soda process, which has been industrially dominating for a long time. Further we refer to US Patent 6 180012 describing a closed tank in which enters C02-rich exhaust and seawater (with NaCl) and in which separately ammonia NH3 is injected, and fresh water is formed. Sodium hydrogen carbonate NaHC03 and ammonium chloride NH4CI precipitate to the 5 bottom and are separated from seawater, which is transformed to fresh water. It may be inefficient not to mix salt water and ammonia NH3 before the injection into the chamber, as the process described in US Patent 6 180012, because the components NH3 and NaCl may not have sufficient time to be effectively mixed before further reaction with C02 in the exhaust gas. Further, it 0 is a disadvantage of the US Patent 6 180 012 that the injection takes place only in a limited upper portion of the tank, and not a more thorough mixing, e.g. in a more extensive portion of the tank. It is a further disadvantage of the US Patent 6 180 012 that the process takes place with inlet of an exhaust gas to a closed tank, because the closed tank will form a counter pressure against the outlet from the gas turbine, and thus there is a risk of a considerable reduction of the gas turbine efficiency.
A typical gas turbine of 25 Megawatt (MW) generates an exhaust flow of about 3,3 kg/s of C02 . That represents a large and undesirable production of C02 considering the probable contributions to greenhouse effects on the global atmosphere. Further, we expect that the unified process according to the invention also will prove commercially healthy because several countries may incur official C02-fees and / or trade C02 emission permissions, so-called "green certificates". The process according to a preferred embodiment of the invention has its greatest potential in those parts of the world in which there is a lack of fresh water, e.g. in the Middle East, Western Africa, The Read Sea, etc. One of the main purposes of the invention is to contribute to the use of liquefied natural gas (LNG), seawater and ammonia for an electricity production of significantly reduced CCVemission, and evaporation of LNG simultaneously with soda production and fresh water production, in which all the products have a sales value. Considering that the invention also improves the efficiency of the electricity production from the gas turbine, by cooling the air to the gas turbine by means of LNG, the invention represents an essential improvement for efficient use of the Solvay process. Further, the process is dependent of low sea water temperature in order to achieve efficient removal of C02, about 10 °C. There is a potential incompatibility in the facts that the seawater temperatures rarely are low in those coastal areas of the world in which there is a lack of fresh water for agricultural purposes or alternatively industrial purposes. Further, there is a potential incompatibility in the facts that evaporation of LNG requires a high seawater temperature, whereas the removal of C02 requires a low seawater temperature. The preferred embodiment of the present invention aims at combining these seemingly counteractive effects, thereby creating an improved process that should be commercially applicable and having a large market potential, particularly in those areas mentioned above.
An article called "Chemical Separation Process for Highly Saline Water, 1. Parametric Experimental Investigation" in Ind. Eng. Chem. Res., 1996, 35, 799-804, describes the separation of highly saline waters under varius contitions and is carried out using a partial-desalting process. The method utilizes a series of chemical reactions involving conversion of Sodium Cloride, the major constituent in saline waters, into sodium bicarbonate, which precipitates under the experimental conditions, and ammonium chloride, which can be separated by crystallization. Experiments of absorption of carbon dioxide in an ammoniated brine have demonstrated the efficiency of the method.
Summary of the invention.
The invention is a method for desalination of salt water, preferably seawater, and separation of C02 from a C02-rich exhaust gas from a fuel combustion engine or gas turbine, comprising the following steps:
LNG is fed into a heat exchanger in which heat is taken from seawater and heat from steam from a steam turbine, and heat from combustion air via a line to the air inlet to a gas turbine, for evaporating LNG to gas being fed to a gas export module and to a fuel gas skid for providing the gas turbine with fuel; In which the combustion air, which at the air supply to the gas turbine thus has a lowered temperature, and thus increases the efficiency of the gas turbine;
In which C02-rich exhaust gas from the gas turbine is led into a chamber or process unit having an inlet with a fan and an outlet for C02-removed exhaust;
In which the cooled salt water from the heat exchanger is fed into the process unit via an upper swivel having vanes that rotates a coaxial feed pipe for seawater and NH4OH, said coaxial pipe being arranged preferably in a centre line in said process unit;
In which NH4OH is fed in via a lower swivel of said insert coaxial pipe and mixed and released with the cooled salt water a series of nozzles at several vertical levels from the coaxial pipe to the upwards streaming and rotating exhaust through the process unit, in order to achieve a good mixture of NH4OH- containing salt water and C02-rich exhaust, for formation of NaHC03, NH4CI, and H20.
The invention is also a process unit for removing CO2 from an exhaust from a combustion engine or gas turbine, comprising the following features: an inlet with a fan and an outlet for exhaust of reduced C02 content; in which cooled salt water can be piped into said process unit via an upper swivel having vanes for rotating a coaxial pipe, said coaxial pipe for seawater and NH4OH feed, said coaxial feed pipe being arranged preferably in a centre line of said process unit; in which NH4OH can be guided in via a lower swivel on said coaxial pipe and mixed with said cooled salt water and released via a series of nozzles from said feed pipe, said nozzles arranged in several vertical levels, to upwardly flowing and rotating exhaust of said process unit; thus for achieving a mixture of NH4OH -containing salt water and C02-rich exhaust for formation of NaHC03, NH CI and desalinated water.
Figure captions.
Attached are figure drawings made for illustrating a preferred embodiment of the invention. However, the figure drawings are not meant for being construed as limiting to the invention, which shall be limited by the attached claims only.
In the drawing figures is used a partially converted petroleum oil tanker as process unit. It is not a condition to the invention that such converted tankers are used, but second hand tankers are cheap and entirely useful under protected conditions, e.g. in an import harbour for LNG for which one requirement may be a protected harbour.
Fig. 1 illustrates a plan section of the terminal limits or process area 26, and illustrates in-flowing fluids and dry matter to the process from the left side in the drawing, with products from the products at the right side in the drawing.
From the left side are illustrated in-flowing fluids and dry components as follows: Chalk Ca(OH) 2 (1) is sent to the process unit for regenerating of ammonia NH3 (19), which will be explained below. Ammonia (2) is sent to a mixing unit for seawater and ammonia, for formation of NH OH for injection via an insert feed pipe (67) to a process unit (17) for removal of C02 from exhaust gas (77) from a gas turbine (7), resulting in release of cleaned exhaust gas (13) to the atmosphere. Central for the preparation to the process is one or more heat exchangers (6). Combustion air of ambient temperature, e.g. 20-35 °C, is led into the heat exchanger. Liquefied natural gas (LNG) (4) from an LNG-storage tank (80) outside of the system, is piped into the heat exchanger (6) while having a temperature of about -163 °C. LNG (4) receives heat from the combustion air (3), and from seawater (5) and from steam from the exhaust gas steam boiler (18), steam of which is also piped through the heat exchanger. The paths of those fluids through the heat exchanger are better illustrated in Fig. 1. Boil-off gas (73) from the storage tank (80) may also be guided in through the heat exchanger if heating is needed before it is fed into the gas skid module (8) to constitute fuel for the gas turbine (7). Possible excess boil-off gas (73) may be fed into a line (29) to a gas export module (10). The heat exchanger (6) is arranged before the gas turbine (7) and the process unit (17) constituting an exhaust process tower (17) for adsorbing C02 from the exhaust, leading further to a precipitation process unit for fresh water at the right side of the drawing.
The process is, according to a preferred embodiment, a method for desalination of salt water (5), which may be seawater or brackish water, with separation of C02 from a C02-rich exhaust (77) from a combustion engine, boiler or gas turbine (7). The process comprises the following steps:
LNG (4) is fed into the heat exchanger (6) in which it receives heat from the seawater (5) and heat from steam (27) from a steam turbine (31), and also heat from combustion air (3) sent via a line (28) to the air inlet (33) to the gas turbine (7). LNG (4) will then receive heat and evaporate to gas (29) that is led to a gas export module (10) and to a fuel gas skid (8) for providing the gas turbine (7) with fuel. The combustion air (28) at the air inlet (33) to the gas turbine (7) thereby is lowered in temperature out of the heat exchanger due to being cooled down by LNG (4), and thus increases the efficiency of the gas turbine (7).
C02-rich exhaust gas (77) from the gas turbine (7) is led into a chamber rather called a process unit (17) having an inlet (35a) provided with a fan (35b) in the lower portion of the process unit (17), and an outlet (74) for C02-removed exhaust (13) at the upper end of the process unit (17).
The cooled salt water (30) from the heat exchanger (6) is fed into the process unit (17) via an upper swivel (40) having vanes that rotate an insert coaxial pipe (67) for seawater and NH4OH in a desired direction (71) being opposite of the desired rotation direction (72) for the exhaust gas, and preferably being arranged along the centre line inside the process unit (17). This increases the degree of mixing between the seawater mixture and the exhaust gas considerably compared to the US Patent 6 180 012.
NH OH is led in through a lower swivel (46) on the coaxial pipe (67). NH4OH is mixed with the cooled salt water (30) and flushed out into the process unit (17) via a series of radially directed nozzles (42) at several vertical levels from the coaxial pipe (67) to the upwardly flowing, rotating exhaust (77) through the process unit (17). As the exhaust (77) is reduced in C02 during the continuous chemical process, we name it C02-lean exhaust (13). By means of the rotating nozzles and the oppositely rotating exhaust, a good mixing of
NH4OH-rich salt water and C02-rich exhaust (77) is achieved, for formation of NaHC03, NH4CI, and H20.
According to a preferred embodiment of the invention the process unit (17) has a diameter increasing with increased elevation from the lower inlet (35a) to the upper outlet (74). Drain gutters (38) to drains (43) are arranged, leading to outlets (45) to a collecting tank (48) for NaHCC»3, NH4CI, and fresh water.
According to a preferred embodiment of the invention, which differs essentially from the mentioned US-Patent 6 180 012 is an exhaust fan (35B) forcing forward the exhaust (77) and thus reduces the counter pressure for the gas turbine (7) so as to compensate the pressure drop through the process unit (17) in order to maintain the efficiency of the gas turbine. The exhaust fan (35B) initiates at the same time a rotation of the exhaust gas (77), further reinforced by means of fixed guide vanes (36) arranged downstream at the inlet (35a) of the process unit (17).
According to the preferred embodiment of the invention NH4OH enters through the lower swivel (46) to a central, coaxial inner pipe (47) in the coaxial feed pipe (67) in the process unit (17). The inner pipe (47) is surrounded by a mantle of salt water (30) through which NH4OH is led out through pipes to sea water ring nozzles (42) in the feed pipe (67). In the nozzles (42) NH4OH and seawater are mixed through flushing from the nozzles to the Cθ2-rich exhaust (77) gradually being changed to C02-lean exhaust (13) on its way upward through the process unit (17). The nozzles are preferably provided with NH4OH- radial distributors (70) arranged just outside the nozzles (42) in order for NH OH to be forced out through an enveloping flow of the mixed cooled seawater (30). This implies two essential advantages relative to US 6 180 012 in that ready- mixed droplets of NH4OH are flushed out towards the NaCI-molecules and contribute to weaken the molecular binding between Na and Cl, thus facilitating formation of NaHC03 as one of the end products.
Precipitated material of NaHC03, NH4CI intermediately dissolved in H20 are conducted to a precipitator (22) for separation of NaHC03 and NH CI from the water H20 which is generally pure fresh water if the process is thoroughly controlled and low temperature of the seawater is maintained. According to a preferred embodiment of the invention the precipitator
(22) is vertically standing and cylindrical, and has a rotation-inducing tangential inlet (25B) for NaHC02 / NH4CI dissolved in water. The driving pressure is generated from the pressure head from the collector tank (48) to the inlet (25B). NaHC02 / NH4CI is precipitated by the rotation and the gravitation towards the bottom of the precipitator (22).
According to a preferred embodiment of the invention fresh water (74) is taken out through a fresh water overflow pipe (75) to a fresh water filter tank (62). The fresh water (74) from the filter tank (62) is sent through a filter (61) to a distribution- and settling tank (60). Salt water may be present at the bottom of the settling tank (60), of which salt water may be lifted back to the seawater pipe (30) by means of the pump (53). Fresh water (74) is pumped by means of the pump (54) to storage tank (59), and further from storage tank (59) via discharge pump (58) and booster pump / export pump (56) to an export pipeline (14). The precipitated NH CI and NaHC03 is lifted by means of a screw pump or "archimedes screw" (51) that is driven by a motor (50), to an outlet (76) from the precipitator (22) to a refining process compartment (64). Chalk Ca(OH)2 (1) is led into the process unit (20) for regeneration of ammonia NH3 that is fed via a pipe (19) to be mixed with additional NH3 (2) from the ammonia tank (65). The ammonia (2, 19) is led further to the mixing unit (32) mixing salt water and ammonia (2, 19) and pumps the mixture NH OH into the feed pipe (67) in the process unit (17).
According to a preferred embodiment of the invention, the gas turbine (7) drives a generator (9) for generating electrical energy that partially may be exported as energy (15), and partially to be used for pumping work, gas and /or C02 export work, and heating a process unit (24) that precipitates soda / Na2C03 (12) for export, and C02 and fresh water, which are exported or returned to the process.
Components list
1 Ca(OH)2 - limestone
2 NH3 - ammonia
3 combustion air to gas turbine(s), e.g.20 °C before the heat exchanger, and after the heat exchanger in to the gas turbine holding 5°C.
4 liquefied natural gas (LNG), -163 °C, (1 ,2 mill, tons/year.
5 seawater - 250000 m3 / day, e.g. 15 °C in to the heat exchanger, and about 5 °C out from the heat exchanger, and further to the rotating feed pipe (67)
6 heat exchanger, (possibly several in parallel). 7 gas turbine(s), (120 MW)
8 gas skid module, for treating gas supply to the gas turbine, (pressurizing, drying and filtering)
9 generator
10 gas export module (needs 25 MW power to deliver 131 MSC FTD (Mill. Standard Cubic Ft. / day (evaporated) LNG/year)
11 CaCI2 - drying agent
12 Na2C03 - soda
13 exhaust out of the process, low in C02 - contents
14 fresh water about 250000 m3 / day 15 electrical energy for export.
16 gas export from the gas export gas export module 10
17 process unit, for adsorption of C O 2 from exhaust
18 exhaust boiler from turbine 7 for generating steam
19 regenerated NH3 - ammonia 20 process unit for regenerating NH3
21 ammonium chloride solution NH4CI
22 process unit for precipitation of sodium hydrogen carbonate NaHC03 and ammonium chloride NH4CI from water
23 sodium hydrogen carbonate NaHC03 24 process unit for precipitation of soda Na2C03 .
25 NaHC03 and NH CI - solution pipe
25B tangential inlet to process unit (22) for precipitation
26 terminal border (extent of the area)
27 steam to heat exchanger (condenser) 28 combustion air to gas turbine (see (3)), about 5 °C
29 gas to gas export module 10 and to fuel gas skid 8
30 seawater to process unit, cooled to about 5°C out from heat exchanger 6
31 steam turbine
32 mixer for seawater and ammonia NH3 33 air inlet to gas turbine
34 muffler (sound attenuator) out from gas turbine 35A inlet [(3§a)] to process unit (17) from exhaust fan (35b) 35B exhaust fan
36 exhaust lead vanes for reinforcing rotation of exhaust gas (77) of high C02- contents
37 drain at lower portion of the process unit (17)
38 guide gutter to drain (43)
39 horizontal and vertical bearing for the rotating coaxial pipe (67)
40 swivel for injection of cooled sea water (30), with guide vanes for rotating the insert feed pipe (67)41 support beams (3 ex) for the feed pipe (67)
41 support beams (3 ex) for the coaxial pipe (67)
42 nozzles for NH4OH and seawater
43 drain from guide gutter (38) 44 horizontal bearing for the rotating feed pipe (67)
45 drop line from the drain (43) to the collector tank (48) for NaHC03 and NH4CI - solution
46 swivel for NH4OH solution
47 supply line for NH4OH to swivel (46) with rotating coaxial pipe (67) with nozzles (42)
48 collecting tank for NaHC03 og NH4CI - solution (25)
49 choke valve at outlet form collector tank (48)
50 motor for screw (Archimedes screw) on lift pump (51 )
51 screw lift pump 52 cofferdam between tanks
53 lift pump for salt-containing water from bottom portion of the distribution / settling tank (60).
54 lift pump for fresh water from distribution /settling tank (60) to fresh water storage tank (54) (59) 55 main deck of (converted) crude oil tanker
56 export booster pump (s) for fresh water
57 pump compartment
58 discharge pump, pressure support to export pump (56)
59 fresh water storage tank 60 distribution tank / settling tank
61 filter between filter tank (62) and distribution / settling tank (60)
62 filter tank
63 drain from precipitation process unit (22)
64 process compartment for precipitated material (76)
65 tank for NH3 ammonia
66 bottom of (converted) crude oil tanker
67 rotating coaxial feed pipe for NH4OH and seawater
68 ring nozzle for sea water (30) in rotating coaxial pipe (67) 69 nozzles for NH4OH on pipe from coaxial supply line (47) in the rotating coaxial pipe (67) in the process unit (17)
70 radial distributor for NH4OH outside of the nozzle (69)
71 rotation direction for the coaxial pipe (67)
72 rotation direction for the exhaust (77) 73 boil-off gas from LNG storage tank
74 fresh water from the distribution / settling tank (60)
75 overflow pipe for water from the separation / process unit (22)
76 outlet of precipitated material sodium hydrogen carbonate NaHC03 and ammonium chloride NH4CI 77 exhaust having a hich C02 - content, in to the process unit (17) from the gas turbine (7)
78 lift pump from the tank (65) which delivers to the mixer (32)
79 turbulence attenuating ribs
79A outlet for exhaust removed of CO2 80 LNG storage tank outside the process plant

Claims

Claims
1. A method for desalinating salt water (5), preferably sea water, and for removing CO2 from a C02-rich exhaust (77) from a combustion engine or gas turbine (7), comprising the following steps:
LNG (4) is fed into a heat exchanger (6) in which said LNG (4) receives heat from the following sources: said salt water (5) that becomes cooled salt water (30); and steam (27) generated from a steam turbine (31); and combustion air (3) from the atmosphere, which is provided via a line (28) to an air inlet (33) of said gas turbine (7); said heat exchanger (6) evaporating said LNG (4) to gaseous form (29), said gas (29) being guided to a gas export module (10); and to a fuel gas skid (8) for supplying fuel to said gas turbine (7); in which said combustion air (3, 28) which, at said air inlet (33) to said gas turbine, has a lowered temperature relative to said combustion air (3) and thus increases the efficiency of said gas turbine (7); in which Cθ2-rich exhaust (77) from said gas turbine (7) is guided into a process unit (17) having an inlet (35a) with a fan (35b) and an outlet (79a) for exhaust (13) of reduced C02 content; in which said cooled saltwater (30) from said heat exchanger (6) is conveyed into said process unit (17) via an upper swivel (40) having vanes for rotating a coaxial pipe (67), said coaxial pipe (67) for distributing seawater and NH4OH feed, said coaxial feed pipe (67) being arranged preferably in a centre line of said process unit (17); in which NH4OH is fed via a lower swivel (46) on said coaxial pipe (67) and mixed with said cooled salt water (30) and released via a series of nozzles (42) from said feed pipe (67), said nozzles (42) arranged in several vertical levels, to upwardly flowing and rotating exhaust (77) of said process unit (17); thus achieving a mixture of NH4OH -containing salt water and C02-rich exhaust (77) for formation of NaHC03, NH4CI and desalinated water.
2. The method according to claim 1 , wherein said process unit (17) has an increasing diametre with increasing elevation from said lower inlet (35a) to said upper outlet (79a), and with draining guide gutters (38) to drains (43) leading to outlets (45) and further to a collector tank (48) for the process unifs (17) products NaHC03, NH4CI and fresh water.
3. The method of claim 2, wherein said exhaust fan (35b) reduces a counter pressure on said gas turbine (7) so that a pressure drop through said process unit (17) is compensated so as to maintain an efficiency of said gas turbine (7).
4. The method of claim 3, wherein said exhaust fan (35b) starts a rotation in said exhaust gas (77), said rotation being reinforced by fixed guide vanes (36) arranged after said inlet (35a) to said process unit (17).
5. The method of claim 1 , wherein said rotation direction of said exhaust (77) and said rotation direction of said coaxial feed pipe (67) are made opposite in order to increase a degree of mixing between exhaust (77) and added fluid (30, 47).
6. The method according to claim 1 or 5, wherein NH4OH enters through said lower swivel (46) to a central, coaxial inner pipe (47) in said coaxial feed pipe (67), said inner pipe (47) being surrounded by a mantle of salt water (30) and in which inner pipe (47) NH4OH is guided out through pipes (69) to seawater ring nozzles (42) of said feed pipe (67), for mixing of NH4OH and seawater in said nozzles (42) during flushing of said NH4OH and said seawater from said nozzles (42), so as to change said exhaust (77) which gradually changes to C02-lean exhaust (13).
7. The method according to claim 6, preferably with an NH4OH -radial distributor (70) arranged just outside said nozzles (42).
8. The method of claim 1 , wherein precipitated material of NaHC03, NH CI and H20 are guided to a precipitator (22) for separating H20 from NaHC03 and NH CI.
9. The method of claim 8, wherein said precipitator (22) is vertically cylindric, having a tangential inlet (25b) for said NaHC03 / NH4CI solution to be precipitated by rotation and gravity toward a bottom of said precipitator (22).
10. The method according to claim 9, wherein fresh water is let out through a fresh water overflow pipe (75) to a fresh water and filter tank (62).
11. The method according to claim 10, wherein said fresh water (74) from said filter tank (62) is allowed to pass through a filter (61) to a distribution tank / settling tank (60).
12. The method of claim 10 or claim 11 , wherein salt containing water from a bottom of said settling tank (60) is lifted back to a seawater pipe (30) using a pump (53).
13. The method of claim 11 , wherein fresh water (74) is pumped by means of a pump (54) to a storage tank (59), and further from said storage tank (59) via a discharge pump (58) to a booster or export pump (56) to an export pipeline (14).
14. The method of claim 9, wherein said precipitated NH4CI and NaHC03 are lifted up by means of a scew pump such as an Archimedes screw (51) being driven by a motor (50), to an outlet (76) from said precipitator (22) to a refining processing compartment (60).
15. The method of claim 1 , wherein limestone, Ca(OH)2, is fed into a process unit (20) for regenerating ammonia, NH3, the ammonia further being guided to said mixing unit (32) via a pipe (19) for mixing with additional NH3 (2), so as to mix salt water and ammonia (2, 19) and pump said mixture of NH4OH into said feed pipe (67) in said process unit (17).
16. A method according to claim 1 , wherein said gas turbine (7) drives a generator (9) and a steam driven generator (31) for generating electrical energy which is partially exported as energy (15) and partially used for pumping work, gas and C02 export work, and heating of H20 in a process unit (24) that precipitates soda/ Na2C03 (12) for export, and C02 and fresh water which is exported or partly returned to the process.
17. A process unit (17) for removing CO2 from an exhaust (77) from a combustion engine or gas turbine (7), comprising the following features: an inlet (35a) with a fan (35b) and an outlet (79a) for exhaust (13) of reduced CO2 content; in which cooled saltwater (30) is piped into said process unit (17) via an upper swivel (40) having vanes for rotating a coaxial pipe (67), said coaxial pipe (67) for seawater and NH4OH feed, said coaxial feed pipe (67) being arranged preferably in a centre line of said process unit (17); in which NH4OH is guided in via a lower swivel (46) on said coaxial pipe (67) and mixed with said cooled salt water (30) and released via a series of nozzles (42) from said feed pipe (67), said nozzles (42) arranged in several vertical levels, to upwardly flowing and rotating exhaust (77) of said process unit (17); thus achieving a mixture of NH4OH -containing salt water and C02-rich exhaust (77) for formation of NaHC03, NH4CI and desalinated water.
18. The process unit of claim 17, wherein said process unit (17) has an increasing diametre with increasing elevation from said lower inlet (35a) to said upper outlet (79a), and with draining guide gutters (38) to drains (43) leading to outlets (45) and further to a collector tank (48) for the process unit's (17) products NaHC03, NH4CI and fresh water.
19. The process unit of claim 17, wherein said rotation direction of said exhaust (77) and said rotation direction of said coaxial feed pipe (67) are opposite in order to increase a degree of mixing between exhaust (77) and added fluid (30, 47).
20. The process unit of claim 17, wherein NH OH enters through said lower swivel
(46) to a central, coaxial inner pipe (47) in said coaxial feed pipe (67), said inner pipe
(47) being surrounded by a mantle of salt water (30) and in which inner pipe (47) NH4OH is guided out through pipes (69) to seawater ring nozzles (42) of said feed pipe (67), for mixing of NH4OH and seawater in said nozzles (42) during flushing of said NH4OH and said seawater from said nozzles (42), so as to change said exhaust (77) which gradually changes to C02-lean exhaust (13).
21. A method for desalinating salt water (5), and for removing CO2 from a C02-ιich exhaust (77) from a combustion engine or gas turbine (7), comprising the following steps: liquefied natural gas, LNG (4), is fed into a heat exchanger (6) in which said LNG (4) receives heat from combustion air (3) from the atmosphere, said combustion air being provided via a line (28) to an air inlet (33) of said gas turbine (7); said heat exchanger (6) evaporating said LNG (4) to gaseous form (29), said gas (29) being guided to a fuel gas skid (8) for supplying fuel to said gas turbine (7); in which said combustion air (3, 28) which, at said air inlet (33) to said gas turbine, has a lowered temperature relative to said air (3) before said heat exchanger (6) , and thus increases the efficiency of said gas turbine (7); in which C02-rich exhaust (77) from said gas turbine (7) is guided into a process unit (17) having an inlet (35a) with a fan (35b) and an outlet (79a) for exhaust (13) of reduced CO2 content; in which said salt water (5, 30) is guided into said process unit (17), via a coaxial feed pipe (67) for seawater and NH4OH feed; and into which NH4OH is guided via said coaxial feed pipe (67) and mixed with said cooled salt water (30) and released from said coaxial feed pipe (67) to flowing exhaust (13) of said process unit (17); thus achieving a mixture of NH4OH -containing salt water and C02-rich exhaust (77) for removing C02 from said exhaust (77), thereby producing said C02-lean exhaust (13) and fresh water.
22. The method of claim 21 , wherein said LNG (4) in said heat exchanger (6) also receives heat from said salt water (5) that becomes cooled salt water (30), said cooled salt water (30) from said heat exchanger (6) is guided into said process unit (17) via said coaxial feed pipe (67) for seawater and NH4OH feed.
23. The method of claim 22, said coaxial feed pipe (67) being arranged in a centre line of said process unit (17).
24. The method of claim 21 , wherein said salt water (5, 30) is fed into said coaxial feed pipe (67) via an upper swivel (40) having rotation vanes for rotating said coaxial pipe (67).
25. The method of claim 21 , wherein NH4OH is guided via a lower swivel (46) on said coaxial feed pipe (67) and mixed with said cooled salt water (30) and released from said coaxial feed pipe (67) via a series of nozzles (42) arranged in several vertical levels, to upwardly flowing and rotating exhaust (13) of said process unit (17);
26. The method of claim 21 , wherein said LNG (4) in said heat exchanger (6) also receives heat from steam (27) generated from a steam turbine (31).
27. The method of claim 21 , wherein said heat exchanger (6) evaporating said LNG (4) to gaseous form (29), said gas (29) being guided to a gas export module (10).
28. The method according to claim 21 , wherein the exhaust flow through said process unit (17) is provided an increasing diametre with increasing elevation from said lower inlet (35a) to said upper outlet (79a), and with draining guide gutters (38) to drains (43) leading to outlets (45) and further to a collector tank (48) for the process unifs (17) products NaHC03, NH CI and H20.
29. The method according to claim 21 , said salt water (5) preferably being seawater.
30. The method according to claim 21 , said process resulting in the formation of NaHC03, NH4CI and fresh water.
31. A method for desalinating salt water (5) and removing C02 from a COVrich exhaust (77) from a combustion engine or gas turbine (7), comprising the following steps: LNG (4) is fed into a heat exchanger (6) in which said LNG (4) receives heat from said salt water (5) that becomes cooled salt water (30), and for evaporating said LNG (4) to gas (29) being guided to a fuel gas skid (8) for supplying fuel to said gas turbine (7); said Cθ2-rich exhaust (77) from said gas tubine (7) is guided into a process unit (17) having an inlet (35a) with a ran (35b) and an outlet (79a) for C02 reduced exhaust (13); said cooled saltwater (30) from said heat exchanger (6) is guided into said process unit (17) having a feed pipe (67) for seawater and NH4OH, said feed pipe having nozzles inside said process unit (17); in which NH4OH is fed through said feed pipe (67) and mixed with said cooled salt water (30) and released from said feed pipe (67) to said process unit's (17) through flowing C02-containing exhaust (77); thus achieving a mixture of NH4OH -contaning salt water and said C02-rich exhaust (77), for formation of fresh water and releasing said C02-reduced exhaust (13) to the atmosphere.
32. The method of claim 31 , wherin, in addition to formation of fresh water, NaHCC»3 and NH4CI are formed in said process unit (17).
33. The method of claim 31 , wherein said LNG (4) in said heat exchanger (6) receives heat from steam (27) from a steam turbine (31).
34. The method of claim 31 , wherein said heat exchanger (6) is evaporating said LNG (4) to gas (29) that partially is guided to a gas export module (10).
35. The method of claim 31 , wherein said LNG (4) in said heat exchanger (6) receives heat from combustion air (3) which thus is cooled and fed via a line (28) to an air inlet (33) to said gas turbine (7),
36. The method of claim 35, wherein said combustion air (3, 28) which, at said air inlet (33) to said gas turbine, has a lowered temperature due to giving heat to said LNG (4) on its way through said heat exchanger (6), and thus becomes more dense and thus increases the efficiency for said gas turbine (7);
37. The method of claim 31 , wherein said feed pipe (67) being coaxial and arranged preferably in a centre line of said process unit (17).
38. The method of claim 31 , wherein NH4OH is guided in via a lower swivel (46) on said feed pipe (67) and mixed with said cooled salt water (30) and released via a series of nozzles (42) in several vertical levels from said feed pipe (67) to said process unifs upward flowing, rotating exhaust (13);
EP03703551A 2002-02-15 2003-02-14 Method and device for desalination of water and removal of carbon dioxide from exhaust gases Expired - Lifetime EP1474364B1 (en)

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NO20020782 2002-02-15
NO20020782A NO317918B1 (en) 2002-02-15 2002-02-15 Process for the preparation of fresh water and purification of carbon dioxide
PCT/NO2003/000059 WO2003068685A1 (en) 2002-02-15 2003-02-14 Method and device for desalination of water and removal of carbon dioxide from exhaust gases

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AT (1) ATE496010T1 (en)
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AU2003206275A1 (en) 2003-09-04
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US7309440B2 (en) 2007-12-18
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US7531144B2 (en) 2009-05-12
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